US1770995A

US1770995A - Process for manufacture of chloride of potassium and carbonates of sodium and potassium

Info

Publication number: US1770995A
Application number: US283405A
Authority: US
Inventors: Robert D Pike; Cummings Ross; Leo V Steck
Original assignee: Individual
Current assignee: Individual
Priority date: 1928-06-06
Filing date: 1928-06-06
Publication date: 1930-07-22
Anticipated expiration: 1947-07-22

Description

July 22, 1930, R. D.A P|KE ET AL PROCESS FOR MANUFACTURE OF CHLORIDE OF POTASSIUM AND CARBONATES OF SODIUM `ND POTASSIUM Filed June 6, 1928 2 Sheets-Sheet IN VEN TOR.

July 22, 1930. R. D. PIKE Er AL 1,770,995 PROCESS FORMANUFACTURE oF CHLORIDE4 0F PoTAssIUM AND CARBQNATES OF SODIUM AND POTASSIUM Filed June 6, 1928 2 Sheets-Sheet 2 of du v2 Patented July 2.2, 193@ onir- 'r masas ROBERT D.' PIKE, OF BIEDMONT, BOSS CUMMINGS; 0F BERKELEY, AND-LEO 'V'. STECK, OF OAKLAND, CALIFORNIA.; SAID CUMMINGS AND SAID STECK ASSIGNORS T SAD) PIKE PROCESS FOR H515 UFAGTUIi-E- OF CHLCBIDE OF POTASIUIII AND CARBONATES 0F SODIUM .AND POTASSIUM.

Application filed June 6, 1928i Serial No. 283,405.

Our present inventionrelates to a process for the manufacture of carbonates of sodium and potassium and chloride of potassium, and more particularly to a process for the manufacture of the above from the natur l resources located in and near Green Rivei, Wyoming.

This application is a continuation in part of a former application filed by uson March 6, 1928, and designated as Serial Number 259,422,which application has been 4formally abandoned.

Near Green River, .Wyoming, there is a large deposit of potassium silicate rock known as wyomingite, of which leucite is the principal potash bearing constituent and at Green River there is available by pumping from shallow wells, a brine composed principally ot sodium carbonate with a lesser content of sodium chloride.

It is an object of our present invention to manufacture from these two important raw materials, or fromflike or analogous materials occurring elsewhere, commercially pure 'chloride of potassium, commercially pure sodium carbonate, and. a brine carrying principally potassium carbonate in solution.

A method for carrying out our invention, in which the sodium carbonate is not produced as such but is circulated in the process, is illustrated in Figure 1 of the accompanying low sheets, in which designates an autoclave or other suitable type of pressure vessel illustrated as a tumbling autoclave adapted to treat ground Wyomingite under agitation and at substantially 200 pounds steam pressure with a mixed solution ot' sodium carbonate and Green River soda brine which is pre ared in a dissolving tank 11, as will liereina ter appear. After treatment in this autoclave for a suitable length of time' to extract from the wyomingite substantially all of the potassium which is subject to hase exchange with sodium. under the conditions obtaining, the pulp is removed to a storage tank 12 and is thence pumped to a continuous filter 13 where the potash bearing Solution is removed from the solids and the latter washed. The washed solids are the tails and are rejected. The solution and Wash water pass to a storage tank 14 whence they are pumped through a set of multiple etl'ect evaporators 15 in counter current to the passage -o`f the vapors therethrough. This Amethod of operating evaporators in counter current is' known as backward feed. In the evaporating process sodium carbonate mono hydrate is salted out and is removed as a pulp from salt boxes 16 of any suitable type and passes to a thickener 17 and thence to a suitable filter ,The clear liquo'r from the filter 18 and thI'e thickener 17 join and pass tothe evaporator supply tank 14. The dewatered sodium carbonate mono' hydrate is transported to the dissolving tank 11, previouslyreferred to, where it is dissolved in the'Green River soda brine. The solution thus formed, together with the ground wyomingite forms the feed to the'autoclave 10.' The strong solution from the last or high pressure eiect of the evaporators 15 goes to the crystallizer 20, where it is cooled to to 30 C. This cooling causes pure KCl to crystallize, the chlorine associated therewith corresponding to the major part of the chlorine which is introduced into the system as sodiumi chloride in the Grreeii` River soda brine.

The pulp from the crystallizer 20 then goes to a-centrifugal separator 21, where KCl crystals are separated out and washed.- The wash water goes to a tank 22 whence it is pumped back to the evaporator supply tank 14. The mother liquor from the centrifuge 21 next goes to a tank 23. It is desirable to have the chloride content o'f this mother liquor as low as ssible, and to have the ratio K2O /N a2() as igh as possible.

In the two quantitative exam les of the carrying out of the method given elow, it is shown, as we have discovered,'that this end is served'by returning in circulation to the evaporator supply tank 14 a portion, preferabl `one-half, of the 'solution from tank 23.

he net advance of solution passing forward from the tank 23 contains all of the potashwhich was removed from the wyomingite in the autoclave 10, except that removed as chloride of potassium (KCl) in 21, almost entirely in the form of potassium carbonate. This finished' potashibrineV can beV employed for the manufacture of commer! cially pure potassium carbonate as disclosed in our copending applicationfiled March 6, 1928,` Serial 'Number 259,423, or for .the manufacture ofcrude mono potassium phosphate as disclosed ina copending' applical tion filedv by Robert D. Pike, March 6, 1928, Serial'Number 259,421. Y

.In both examples of carrying out our -process described below, the following are the analyses of the Green River soda brine and wyomingite respectively:

Green. River soda brine 'lhe wyomingite is ground dry to have the following screen analysis:

Percent *10+ 14 0.3 -14-1- 20 4.0 00+ 28 10.4 28+ 35 10.9 35+ 48 12.2 -4S+ S5 7.0 65+100 7.8 -100+1G0 0.4 .-150-t200 6.5 -200 35.5

Example No. 14

One quarter of solution from tank 23 is returned in circulation to tank 4. The feed to the autoclave 10 is in batches-which per 100 pounds wyoniingit'e follow:

v Pounds W yomingite 10) Return sodium carbonate mono hydrate 21.3 Green River soda brine 100.8

. After the treatment in the autoclave 10, the removal and washing of the tails and the addition of the return solution from tank 23 and the wash waters, the composition of the evaporator' feed per ton' (200G pounds) of Kzo, produce-a s Koi crysaii alla a5 Kzco3 inthe finishedbrine, is as follows:

Koi 777 KzcoDA -1 -A 2988 nazcoa 5514. .H20 u aosoo A. method for producing fromsuch' a solution pure crystals of KCl and NagCOaHzO on the one hand and a substantially pure brine of KZCO3 on the other, has not hitherto been known and discovery of such a method' conf stitutes one of the principal features of our invention. We have discovered'that if this brine b e evaporated preferably at, or nearly at, atmospheric-boiling temperatures, until the liquor becomes saturated with reference to both KCl and Na2GO3, there will crystallize out during this process of concentration 5440 pounds of pure Na2CO3H2O per tonof KZO as above defined, and that Vthe water evaporated will amount to 25,331 pounds. Furthermore no crystallization of the NagCOal-LO occurs until there have been evaporated 13,255

ounds of water. In carrying out the process 1n multiple effect evaporators, backward feed is employed so that the crystals of NazCOa'I-LO will form in the effects boiling at the higher temperatures. This procedure insures the production of a quick settling and free filtering. crystal. d

' The strongsolution from the evaporator contains the'following per -ton of KZO. as above defined.

' Pounds KCI 777 KgCOS i NLQCOS H2O 437 9 This solution has a specific gravity hot of 1.527 and boils at atmospheric pressure at 120 C. We have discovered that if this solution is cooled in mechanicalcrystallizers to 25 C. fairly rapidly, pure KCl crystallizes, in spite of the fact that the stable solid phase, which should be in equilibrium with the resulting solution accordingr to Blasdale, .l our; Am. Chem. Soc. 45, 2935 (1923), is

. 1 KNaCO36H2O. The mother liquor remains supersaturatec with respect to this latter salt and pure KCI crystals are recovered by entrifuging- The solution from the crystallizer 20 conf tains the following per ton of-KEO as above defined:

Pounds KCI 123 Kzco. 2988, Na2CO3 875 H20 4379.

One-quarter of this-solution is returned in circulation to the evaporator feed and the balance is the net brine produced by the process llO ` Ero/mpio No. 2 Gnemhalt ot the solution 'from tanlr 23 is returned in circulation to tanlr le.

The feed to the autoclave 10 per 100 pounds et wyoniingite is as follows: i

lounds VVyomingite 100 Return sodium carbonate mono hydrate 22.2 Green River soda brine 97.

Pounds' KCI fito KZCO, 453B rotzooi este H20 31400 After evaporating in the sanie ina-nner' as "described under Example 1, a strong solution is produced which contains per ton K2O, as above defined, the following:

Pounds" KCl 7?@ KZCS 4538 Nagclg i HZG 5660 lt this solution is cooled as above described to 250 C. it remains supersat-urated to the sta-ble solid phase, KNaCO36l-l2,'and pure KCl is crystallized. After this is removed by centrituging, there remains in the mother liquor porton of K2@ as above deiined, the following:

. Pounds KC1 123 KZCOS 4538 Naso?, ieee Ho@ i- One-halt of this solution is returned in circulation to the evaporator 'feed and the balance is the net brine produced by the process.

The effect of increasing the circulation of strong brineafter crystallizing the KCI is illustrated in the following summary.

Raum 01% 0i herum of i@ of strong brine strong brine M01 mno ino/NMO 2.723 3.2 M01 :aan coa/en :ner A .51.6

vlierred to.

Uur process is applicable to leaching with brines containing lesser or greater amounts et NaCl and greater or lesser amounts or Na2C03 than 'the Green River soda water., .As the content of NaCl decreases, the amount of liquor which it is necessary to circulate from tanlr 23 to tanlr 1d, so as to produce a potassium carbonate brine of desired purity decreases until in the limiting case when the leach liquor is all sodium carbonate with no sodium chloride it is unnecessary to employ circulation in order to produce a brine in which the mol ratio X20/Naz@ is greater than 3; and, in such limiting case, the crystallizer 20 would be eliminated and the strong liquor from the evaporator'would be the iinished carbonate brine. 0n the other hand, as the sodium chloride content in the leaching brine increases, a point is speedily reached where the flow sheet of Figure 1 is no longer adequate to produce a potassium carbonate brine of the desired purity, but the latter will contain undesirably large amounts of both sodium carbonate and potassium chloride. y

li' lthe sodium carbonatev mono hydrate, instead of being returned in circulation in 'the process, is removed and washed tree 4trom mother liquor, it is a commercially pure salt which can be used as such, or easily converted to soda ash or caustic soda. .To do this, therefore, constitutes a valuable variation of our process; but in so doing, the leaching brine becomes .the Green River soda brine in which no sodium carbonate has been dissolved. 'ln etlect, therefore, the leaching brine which goes to the autoclave contains much more sodium chloride in rela-` tion to sodium carbonate than is the case in Figure 1, and the solution of this case, using the Green River soda brine, isvirtually also the solution of the case involving the use of the flow sheet of Figure 1 with a brine containing a rnuch larger amount of sodium chloride than the Green River brine.

Figure 2 shows a dow sheet for use of the Green River soda brine for leaching wyorningte ini-which all et the sodium carbonate mono hydrate is removed. ln Figure, 25 is .a storage tank for the Green 'River soda brine, from whence it is fed through a, preliminary Vevaporator 26, where of its water is evaporated amountin to about 34,800 pounds per ton (2000 pounds of total K2@ which is eventually produced by the process as the chloride and the carbonate.l The concentrated brine is the leach solution and is stored in a tanlr 27, and then goes to a/leaching plant 28 whence it is introduced together with ,ground wyomingite into the autoclave, as

previously described. The treatment in the leaching plant is the same as in dow sheet Figure 1 and after liltration and washing et the tails the combined Wash water goes to a primary evaporator storage OO AU- For each tou of potash produced. there are required about 25,000 pounds ot ivyemingite and 30,050 pounds concentrated brine containing:

Pounds Nag@ as NaCl 804;

Nag@ as llagCQa 3608 lllfatelg; 26233 Pounds KCl 1934 KZCOS 1141 NagCOa 5297 H2() after addition of Wash 34400 From tank 29 the liquor passes through primary salting out evaporators 30. lThese evaporators are operated on `the counter current principle, and the sodium carbonate mono hydratejvhich is salted out is removed. The latter is treated by suitable standard apparatus, not illustrated, for separation from the mother liquor and drying. rllhe primary evaporators produce about Li060 pounds NagCUal-LO and evaporate about 25,000 pounds of Water. The strong liquor from the primary evaporator 30 goes to a primary crystallizer 31 Where it is cooled to from 25o to 30o C. producing about 1140 pounds KCl. The latter is removed and freed from the mother liquor by suitable Well known apparatus not illustrated and the mother liquor goes to a secondary evaporator storage 32.

From the secondary evaporator storage tank 32 the liquor goes to secondary evaporators 33 Where about v1225 pounds of NazCCgHzO is salted out and about 5000 pounds of Water is evaporated. These secondary evaporators also Work on the counter current principle. The strong liquor then goes to a secondary crystaliizer 34 Where it is cooled to a temperature of 25 to 30 C. and about 765 pounds of KCl is salted out. The latter is removed from the primary crystillizer and of the clear liquor is returned in circulation to the storage tank 32, the remaining 20% constituting the net yield of potassium carbonate. By the above procedure We have found that the final carbonate brine is made to contain only a trace of KCl and to have a mol ratio of R20/Naz@ of about 3.26/1.

The net brine is made up as follows:

Pounds KCI 29 KZCO,l 1141 Na()a 265 Of the total K2() produced, about 00% is as the chloride a0 /0 the carbonate, l ifo-r each ton of K2() there are produced 885 pounds la 3HE@ null be observed tha;l the ratio is substantially the same in the otassium carbonate brine produced by the ew sheet oi Sfigurc 2 as by that of Figure l.

't Will be understood that our process is applicable to any potassium silicate mineral Whose potassium is amenable to base exchange with. sodium, and to any leaching brine carrying principally the carbonates and chlorides of sodium, and. Whenever the terms wyomingite and Green River soda brine are employed inthe appended claims, it will be understood that like or analogous materials are included.

--laving thus described our invention what We claim and desire to secure by Letters latent is- 1. A process for producing a` carbonate brine containingT a predominating amount of potassium carbonate from Wyomingite and a brine composed principally of a solution of sodium carbonate in Water, which consists in grinding Wyomingite and leaching under steam pressure With the said brine, removing the leach solution from the solids, evaporating so as to crystallize out sodium carbonate mono hydrate and removing crystals of the latter salt until the mol ratio K20/Na20 in the mother liquor is greater than 2.

2. A. process for treating the system NaKZCGClQHZO for separation of NaZCOgHEO, KCl and KgCOa Which consists in evaporating to salt out Na2CO3H2O, cooling the mother liquor to salt out KCl crystals, evaporating the remaining mother liquor in a secondary evaporator to salt out additional NagCOSHZO, 'cooling the mother liquor to salt out additional KCl, and circulating a portion of the last named mother liquor back through the secondary evaporator, thus leaving a brine carrying principally KZC/O3.

3. In a 'process for producing salts of potassium and sodium by leaching potassium silicate base exchange minerals with a brine carrying principally the carbonatos and chlorides of sodium, the steps of separating the sodium carbonate, potassium carbonate and potassium chloride respectively, which consist in evaporating the leach liquor so as to ,crystallize out sodium carbonate mono hydratel, and then cooling the mother liquor to' crystallize out substantially, pure potassiumchloride, evaporating the remaining mother liquor in a secondary evaporator to salt outadclitional NaZCOSHZO, and cooling the mother liquor to salt out additional KCl, leaving a brine carrying principally potassium carbonate.

Il. n a process for producing salts of pon.. c. (s

tassium and. sodium by leaching potassium silicate base exchange minerals with a brine carrying principally the carbonates and chlorides of sodium, the steps for separating the sodium carbonate, potassium carbonate and potassium chloride respectively, which consist in evaporating the leach liquoreso as to crystallize out sodium carbonate mono hydrate, ami then cooling the mother liquor to crystallize out substantially pure' potassium chloride, evaporating the remaining mother liquor in a secondary evaporator to salt out additional NaZCOBHZO, cooling the mother liquor to salt out additional KCl, and circulating a portion of the last namedmother liquor back through the secondary evaporator, leaving a brine carrying principally potassium carbonate. ROBERT D. PIKE.

ROSS CUMMINGS. LEO V. STECK.